Comparison of Catalytic Cracking Performance between Riser Reactor and Microactivity Test (MAT) Unit

2001 ◽  
Vol 15 (4) ◽  
pp. 783-785 ◽  
Author(s):  
Siauw Ng ◽  
Hong Yang ◽  
Jinsheng Wang ◽  
Yuxia Zhu ◽  
Craig Fairbridge ◽  
...  
Keyword(s):  
Catalytic Cracking ◽  
Riser Reactor ◽  
Cracking Performance

scholarly journals A diffusion anisotropy descriptor links morphology effects of H-ZSM-5 zeolites to their catalytic cracking performance

2021 ◽  
Vol 4 (1) ◽  
Author(s):  
Xiaoliang Liu ◽  
Jing Shi ◽  
Guang Yang ◽  
Jian Zhou ◽  
Chuanming Wang ◽  
...  
Keyword(s):  
Catalytic Activity ◽  
Catalytic Cracking ◽  
Catalytic Performance ◽  
Zeolite Catalysts ◽  
Time Resolved ◽  
Cracking Performance ◽  
Morphology Effect ◽  
Ft Ir ◽  
The Difference ◽  
Dynamics Simulations

AbstractZeolite morphology is crucial in determining their catalytic activity, selectivity and stability, but quantitative descriptors of such a morphology effect are challenging to define. Here we introduce a descriptor that accounts for the morphology effect in the catalytic performances of H-ZSM-5 zeolite for C4 olefin catalytic cracking. A series of H-ZSM-5 zeolites with similar sheet-like morphology but different c-axis lengths were synthesized. We found that the catalytic activity and stability is improved in samples with longer c-axis. Combining time-resolved in-situ FT-IR spectroscopy with molecular dynamics simulations, we show that the difference in catalytic performance can be attributed to the anisotropy of the intracrystalline diffusive propensity of the olefins in different channels. Our descriptor offers mechanistic insight for the design of highly effective zeolite catalysts for olefin cracking.

scholarly journals Role of Catalyst in Optimizing Fluid Catalytic Cracking Performance During Cracking of H-Oil-Derived Gas Oils

ACS Omega ◽  
2021 ◽  
Author(s):  
Dicho Stratiev ◽  
Ivelina Shishkova ◽  
Mihail Ivanov ◽  
Rosen Dinkov ◽  
Borislav Georgiev ◽  
...  
Keyword(s):  
Catalytic Cracking ◽  
Fluid Catalytic Cracking ◽  
Cracking Performance

Mathematical modelling of catalytic cracking riser reactor

2017 ◽  
Vol 329 ◽  
pp. 262-274 ◽  
Author(s):  
Emiliya Ivanchina ◽  
Elena Ivashkina ◽  
Galina Nazarova
Keyword(s):  
Mathematical Modelling ◽  
Catalytic Cracking ◽  
Riser Reactor

scholarly journals Catalytic Cracking of Biodiesel Waste Using Metal Supported SBA-15 Mesoporous Catalysts

Catalysts ◽  
2019 ◽  
Vol 9 (3) ◽  
pp. 291 ◽  
Author(s):  
Duangkamon Jiraroj ◽  
Tunyatorn Tongtooltush ◽  
Joongjai Panpranot ◽  
Piyasan Praserthdam ◽  
Duangamol Tungasmita
Keyword(s):  
Electron Microscopy ◽  
Catalytic Cracking ◽  
Liquid Fraction ◽  
Batch Reactor ◽  
Biodiesel Production ◽  
Gaseous Products ◽  
Pure Glycerol ◽  
Transmission Electron ◽  
N2 Atmosphere ◽  
Cracking Performance

Palladium (Pd) and aluminium (Al) supported on SBA-15 were prepared as catalysts for cracking biodiesel waste from biodiesel production. Mesoporous silica SBA-15 was first synthesized by a hydrothermal method and then loaded with Al or Pd particles were loaded using postsynthesis or aqueous wet impregnation methods, respectively. The physical properties of the catalysts were characterized by X-ray diffraction (XRD), nitrogen (N2) adsorption, scanning electron microscopy (SEM), and transmission electron microscopy (TEM) analyses. The catalytic cracking performance of biodiesel waste was evaluated at reaction temperatures above 400 °C under a N2 atmosphere in a batch reactor for 40 min in comparison with that for pure glycerol, where the conversion of biodiesel waste reached 86.8% with 10 wt% Pd-SBA-15 at 650 °C. The product types depended on whether the starting material was pure glycerol or biodiesel waste. The main gaseous products were carbon monoxide as synthesis gas, carbon dioxide, and 1,3-butadiene. Additionally, 2-cyclopenten-1-one and 2-propen-1-ol were major products in the liquid fraction, which can be used in pharmaceuticals and as a flame retardant, respectively.

scholarly journals Distribution of nitrogen and oxygen compounds in shale oil distillates and their catalytic cracking performance

2020 ◽  
Vol 17 (6) ◽  
pp. 1764-1778
Author(s):  
Xiao-Bo Chen ◽  
Xin-Yang Zhang ◽  
Ru-Meng Qin ◽  
Sheng-Jie Shan ◽  
Pan-Deng Xia ◽  
...  
Keyword(s):  
Catalytic Cracking ◽  
Carbon Number ◽  
Negative Ion ◽  
Ion Cyclotron Resonance ◽  
Shale Oil ◽  
Basic Nitrogen ◽  
Liquid Products ◽  
Cracking Performance ◽  
Heteroatomic Compounds ◽  
Ft Icr Ms

AbstractThe positive- and negative-ion electrospray ionization (ESI) coupled with Fourier transform-ion cyclotron resonance mass spectrometry (FT-ICR MS) was employed to identify the chemical composition of heteroatomic compounds in four distillates of Fushun shale oil, and their catalytic cracking performance was investigated. There are nine classes of basic nitrogen compounds (BNCs) and eleven classes of non-basic heteroatomic compounds (NBHCs) in the different distillates. The dominant BNCs are mainly basic N1 class species. The dominant NBHCs are mainly acidic O2 and O1 class species in the 300–350 °C, 350–400 °C, and 400–450 °C distillates, while the neutral N1, N1O1 and N2 compounds become relatively abundant in the > 450 °C fraction. The basic N1 compounds and acidic O1 and O2 compounds are separated into different distillates by the degree of alkylation (different carbon number) but not by aromaticity (different double-bond equivalent values). The basic N1O1 and N2 class species and neutral N1 and N2 class species are separated into different distillates by the degrees of both alkylation and aromaticity. After the catalytic cracking of Fushun shale oil, the classes of BNCs in the liquid products remain unchanged, while the classes and relative abundances of NBHCs vary significantly.

Catalytic Cracking of n-Hexane over MeAPOs Molecular Sieves

2011 ◽  
Vol 236-238 ◽  
pp. 1063-1066
Author(s):  
Li Li Feng ◽  
Chong Chen Wang ◽  
Xing Yi Qi
Keyword(s):  
Molecular Sieves ◽  
Catalytic Cracking ◽  
Contact Time ◽  
Hydrothermal Crystallization ◽  
Reaction Conditions ◽  
First Order ◽  
Crystallization Method ◽  
Cracking Performance ◽  
Conversion Level ◽  
Hexane Concentration

Mg-, Zn-, and Cu-substituted aluminophosphate molecular sieves (MeAPO-5 and MeAPO-11) were synthesized by hydrothermal crystallization method. Then-hexane cracking performance over the as-prepared MeAPOs was estimated under different reaction conditions. MeAPO-5 molecular sieves exhibited higher activity for the cracking conversion in the temperature range of 723~823 K than MeAPO-11. The conversion level ofn-hexane over MeAPOs with the same topology had the following order: MgAPOs > ZnAPOs > CuAPOs. The cracking results showed that the conversion level ofn-hexane increased with increasing reaction temperatures and contact time, and that the first order is determined in then-hexane concentration.

Preparation of Y Zeolite-Based Catalysts and their Catalytic Cracking Performances of Venezuelan Heavy Oil

2012 ◽  
Vol 608-609 ◽  
pp. 1407-1412
Author(s):  
Peng Hui Zeng ◽  
Bao Jian Shen ◽  
Sheng Fu Ji ◽  
Yun Liang ◽  
Xiang Hai Meng
Keyword(s):  
Pore Structure ◽  
Heavy Oil ◽  
Catalytic Cracking ◽  
Product Distribution ◽  
Pore Distribution ◽  
Oil Yield ◽  
Y Zeolite ◽  
Acidic Properties ◽  
Cracking Performance ◽  
Adsorption Desorption

Five kinds of modified Y zeolite-based fluid catalytic cracking (FCC) catalysts were prepared. The N2 adsorption desorption and NH3 temperature-programmed-desorption (NH3-TPD) were used to investigate the pore structure and acidic properties of the catalysts. The effects of pore structure and acidic properties of catalysts on the catalytic cracking performance of Venezuelan heavy oil were carried out using an advanced cracking evaluation unit. The results of N2 adsorption desorption and NH3-TPD show that CAT-A and CAT-B catalysts with rundle pore distribution have a similar pore sizes and acidSubscript textSubscript textic properties. The catalytic cracking results show that the acidic properties and the pore distribution of the catalysts have obvious effects on the conversion and product distribution. The light oil yield and total liquid oil yield can reach 58.75wt% and 73.83 wt%, respectively, under reaction temperature of 520°C.

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